AU2007251608A1 - A process for the manufacture of carbon disulphide - Google Patents
A process for the manufacture of carbon disulphide Download PDFInfo
- Publication number
- AU2007251608A1 AU2007251608A1 AU2007251608A AU2007251608A AU2007251608A1 AU 2007251608 A1 AU2007251608 A1 AU 2007251608A1 AU 2007251608 A AU2007251608 A AU 2007251608A AU 2007251608 A AU2007251608 A AU 2007251608A AU 2007251608 A1 AU2007251608 A1 AU 2007251608A1
- Authority
- AU
- Australia
- Prior art keywords
- carbon disulphide
- liquid
- process according
- sulphur
- reaction zone
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
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- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 title claims description 86
- 238000000034 method Methods 0.000 title claims description 38
- 238000004519 manufacturing process Methods 0.000 title claims description 9
- 239000007788 liquid Substances 0.000 claims description 54
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 43
- 239000005864 Sulphur Substances 0.000 claims description 43
- 238000006243 chemical reaction Methods 0.000 claims description 36
- 150000001875 compounds Chemical class 0.000 claims description 34
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 16
- 239000012071 phase Substances 0.000 claims description 16
- 238000011084 recovery Methods 0.000 claims description 15
- 239000007792 gaseous phase Substances 0.000 claims description 12
- 229930195733 hydrocarbon Natural products 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 9
- 239000004215 Carbon black (E152) Substances 0.000 claims description 8
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 6
- 125000004432 carbon atom Chemical group C* 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 2
- 229910001882 dioxygen Inorganic materials 0.000 claims description 2
- 239000003921 oil Substances 0.000 description 18
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 7
- 239000007789 gas Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical group N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 229910052757 nitrogen Chemical group 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 101100293720 Caenorhabditis elegans ncs-2 gene Proteins 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical class [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 241000237858 Gastropoda Species 0.000 description 1
- 229920000297 Rayon Polymers 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- -1 asphalthenes Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 229940125810 compound 20 Drugs 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- JAXFJECJQZDFJS-XHEPKHHKSA-N gtpl8555 Chemical compound OC(=O)C[C@H](N)C(=O)N[C@@H](CCC(O)=O)C(=O)N[C@@H](C(C)C)C(=O)N[C@@H](C(C)C)C(=O)N1CCC[C@@H]1C(=O)N[C@H](B1O[C@@]2(C)[C@H]3C[C@H](C3(C)C)C[C@H]2O1)CCC1=CC=C(F)C=C1 JAXFJECJQZDFJS-XHEPKHHKSA-N 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000002964 rayon Substances 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 229930192474 thiophene Natural products 0.000 description 1
- 150000003577 thiophenes Chemical class 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
Classifications
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/70—Compounds containing carbon and sulfur, e.g. thiophosgene
- C01B32/72—Carbon disulfide
- C01B32/75—Preparation by reacting sulfur or sulfur compounds with hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
- C09K8/00—Compositions for drilling of boreholes or wells; Compositions for treating boreholes or wells, e.g. for completion or for remedial operations
- C09K8/58—Compositions for enhanced recovery methods for obtaining hydrocarbons, i.e. for improving the mobility of the oil, e.g. displacing fluids
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Mining & Mineral Resources (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Physics & Mathematics (AREA)
- Environmental & Geological Engineering (AREA)
- Fluid Mechanics (AREA)
- Inorganic Chemistry (AREA)
- Geochemistry & Mineralogy (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Lubricants (AREA)
Description
WO2007/131976 PCT/EP2007/054610 A PROCESS FOR THE MANUFACTURE OF CARBON DISULPHIDE The present invention provides a process for the manufacture of carbon disulphide and the use of a liquid stream comprising carbon disulphide and hydrogen sulphide obtainable by such process for enhanced oil recovery. 5 Carbon disulphide is typically manufactured by reacting a lower hydrocarbon with elemental sulphur that is in the vapour phase according to the reaction equation: CnH2(n+1) + (3n+1)S 4 nCS 2 + (n+1)H 2 S (1) 10 In GB 1,173,344 for example is disclosed a process for reacting vapour phase sulphur and propane in the absence of a catalyst under a pressure not exceeding 10 atmospheres in a reaction zone which is maintained at a temperature of 550 to 850 'C. 15 In US 3,087,788 is disclosed a process for producing carbon disulphide from hydrocarbon gas and vaporous sulphur in a non-catalytic reaction stage combined with, preferably followed by, a catalytic reaction stage, wherein both stages are operated at a pressure between 2 20 and 20 atmospheres and a temperature between 400 and 750 oC. It is also known to manufacture carbon disulphide by catalytically reacting liquid sulphur with a hydrocarbon. In US 2,492,719 for example is disclosed a process for 25 preparing carbon disulphide, wherein a suspension of catalyst in molten sulphur is contacted with a hydrocarbon gas at a temperature of approximately 500 to 700 oC, under sufficient pressure to maintain the sulphur in liquid phase. 30 Carbon disulphide is known to be a suitable solvent for enhanced oil recovery by miscible flooding. In enhanced oil recovery by miscible flooding, a solvent for WO2007/131976 PCT/EP2007/054610 - 2 oil is introduced into an oil reservoir and driven through the reservoir to increase oil recovery from the reservoir beyond what can be achieved by conventional means. In US 3,847,221 for example, the use of carbon 5 disulphide for enhanced oil recovery from tar sands is disclosed. It has now been found that carbon disulphide can be manufactured with an attractive yield by reacting liquid sulphur with a hydrocarbon in the absence of a catalyst. 10 Accordingly, the present invention provides a process for the manufacture of carbon disulphide comprising supplying a feedstock comprising a hydrocarbonaceous compound to a reaction zone containing a liquid elemental sulphur phase and reacting, in the liquid sulphur phase, 15 at a temperature in the range of from 350 to 750 oC and a pressure in the range of from 3 to 200 bar (absolute) and in the absence of a catalyst, the hydrocarbonaceous compound with elemental sulphur in the absence of molecular oxygen. 20 An advantage of the process according to the invention is that it can be carried out in the absence of a catalyst. Compared to the conventional vapour phase process for carbon disulphide production, the process according to 25 the invention has the advantage that there is no need to vaporise the sulphur. In the process according to the invention, a gaseous phase comprising carbon disulphide and hydrogen sulphide is obtained. The gaseous phase may also comprise 30 unconverted hydrocarbonaceous compound and elemental sulphur. By subjecting the gaseous phase to a single or sequential condensation steps, a liquid stream comprising carbon disulphide and hydrogen sulphide is obtained from the process according to the invention that may suitably 35 be used for enhanced oil recovery.
WO2007/131976 PCT/EP2007/054610 - 3 Accordingly, the present invention further provides the use of a liquid stream comprising carbon disulphide and hydrogen sulphide for enhanced oil recovery, the liquid stream being obtainable by a process as 5 hereinabove defined. In the process according to the invention, carbon disulphide is produced by reacting a hydrocarbonaceous compound with elemental sulphur in a reaction zone containing a liquid elemental sulphur phase. The reaction 10 between hydrocarbonaceous compound and elemental sulphur is carried out in the liquid sulphur phase. The reactants are reacted with each other at a temperature in the range of from 350 to 750 oC and at a pressure sufficient to maintain a liquid elemental sulphur phase. 15 The reaction is suitably carried out in a standard chemical reactor, e.g. a tank reactor. Such a reactor usually comprises a vertical, tubular reactor. The length/diameter ratio may vary from 20/1 to 1/3, and is suitably between 10/1 and 1/1, e.g. between 5/1 and 20 1.5/1. The hydrocarbonaceous feedstock is introduced at the lower end of the reactor, at least at a level lower than the middle of the expanded liquid sulphur column. Preferably the hydrocarbonaceous feed is introduced into the lower third of the expanded liquid sulphur column, 25 more preferably into the lower quarter, e.g. at 10% of the height of the expanded liquid sulphur column or even lower. The reaction between the hydrocarbonaceous feed and the sulphur takes place within the boundaries in the reactor of the expanded liquid sulphur phase. The process 30 of the invention comprises fixed reactors, rotating reactors are not used. A feedstock comprising a hydrocarbonaceous compound is supplied to the reaction zone containing the liquid elemental sulphur phase. Reference herein to a 35 hydrocarbonaceous compound is to a compound having carbon WO2007/131976 PCT/EP2007/054610 -4 and hydrogen atoms and, optionally, a smaller amount of heteroatoms such as oxygen, sulphur or nitrogen. The hydrocarbonaceous compound may be gaseous, liquid, or solid at the reaction conditions applied. Examples of 5 suitable hydrocarbonaceous compounds are hydrocarbons, asphalthenes, mercaptans, thiophenes, and alkylpolysulphides. Preferably, the hydrocarbonaceous compound is gaseous at the reaction conditions applied. Preferably, the hydrocarbonaceous compound is a 10 hydrocarbon, more preferably a saturated or unsaturated aliphatic hydrocarbon, more preferably an aliphatic hydrocarbon with in the range of from 1 to 20 carbon atoms. Saturated hydrocarbons with 1 to 4 carbon atoms, in particular methane, ethane, and propane, are 15 particularly suitable reactants in the process according to the invention. In the process according to the invention, the hydrocarbonaceous compound and elemental sulphur react with each other. In case the hydrocarbonaceous compound 20 is a saturated aliphatic hydrocarbon, the reaction is according to the overall reaction equation: CnH2(n+1) + (3n+1)S 4 nCS 2 + (n+1)H 2 S The feedstock may comprise more than one hydrocarbonaceous compound. The feedstock may also 25 comprise other compounds, for example hydrogen sulphide, carbon oxides, and inert gases such as nitrogen and helium. Examples of suitable feedstocks for the process according to the invention are natural gas, liquefied propane gas (LPG), atmospheric or vacuum distillates, 30 heavy oil streams such as the residuum obtained after atmospheric and/or vacuum distillation of crude oil, mercaptan-containing off-gas from a mercaptan absorber. A particularly suitable hydrocarbonaceous compound comprising feedstock is natural gas.
WO2007/131976 PCT/EP2007/054610 -5 In the process according to the invention, the feedstock will typically be continually supplied to the reaction zone. In case the hydrocarbonaceous compound is solid at the reaction conditions applied, the feedstock 5 is preferably supplied to the reaction zone by pre-mixing it with the liquid sulphur phase with which the reaction zone is to be filled. This may also be done in case of a hydrocarbonaceous compound that is liquid at the reaction conditions applied. Preferably, a liquid feedstock is 10 continually supplied to the reaction zone. In case of a gaseous feedstock, the process may be carried out in any reactor configuration suitable for gas-liquid contacting, typically by bubbling the gaseous reactants through a reactor filled with liquid sulphur. 15 In order to prevent the formation of gas slugs, the reactor may contain solid contactors, for example a structured packing or gauzes. For a gaseous hydrocarbonaceous compound, the initial contact time of the hydrocarbonaceous compound with the liquid sulphur is 20 preferably in the range of from 0.1 to 200 seconds. It will be appreciated that the optimal contact time will increase with the refractive nature of the hydrocarbonaceous compound. A hydrocarbonaceous compound that is solid at the reaction conditions applied will 25 therefore generally require a longer contact time than a hydrocarbonaceous compound that is liquid at the reaction conditions applied and a liquid compound will require a longer contact time than a gaseous compound. A stream of liquid make-up sulphur may be 30 continuously supplied to the reaction zone. Alternatively, the elemental sulphur in the reaction zone is periodically refreshed. Usually the amount of liquid sulphur will comprise 10-90 vol% of the total reactor volume, preferably 20-80 vol%, more preferably 30 35 70 vol%.
WO 2007/131976 PCT/EP2007/054610 - 6 The process according to the invention is carried out at a temperature in the range of from 350 to 750 oC, preferably of from 400 to 700 oC, more preferably of from 400 to 650 oC, especially between 500 and 550 oC. 5 The reactants are reacted with each other at a pressure that is sufficient to maintain a liquid elemental sulphur phase. Therefore, the pressure strongly depends on the reaction temperature. Preferably, the pressure is in the range of from 3 to 200 bar (absolute), 10 more preferably of from 5 to 100 bar (absolute), even more preferably of from 5 to 30 bar (absolute). In the process according to the invention, a gaseous phase mainly comprising carbon disulphide, hydrogen sulphide, and elemental sulphur is formed. In case a 15 gaseous hydrocarbonaceous compound is used, the gaseous phase typically also comprises unconverted hydrocarbonaceous compound. Preferably, the process according to the invention further comprises withdrawing the gaseous phase 20 comprising carbon disulphide and hydrogen sulphide from the reaction zone and condensing at least part of the gaseous phase to obtain a liquid stream comprising carbon disulphide. If the effluent of the reaction zone is a mixed 25 liquid and gaseous effluent, such as may for example be the case if a liquid feedstock is supplied to the reaction zone, the gas and the liquid phases of the effluent will first be separated in a gas-liquid separator. 30 The withdrawn gaseous phase may be condensed to obtain a liquid stream comprising carbon disulphide. Preferably, the gaseous phase is subjected to sequential partial condensation steps to obtain a liquid stream with a higher concentration of carbon disulphide. Purification 35 steps other than condensation may also be applied in WO2007/131976 PCT/EP2007/054610 -7 order to obtain a liquid stream comprising carbon disulphide with the desired composition. Preferably, the gaseous phase withdrawn from the reaction zone is first cooled at super-atmospheric 5 pressure to a temperature at which elemental sulphur condenses whilst carbon disulphide and the other components remain in the sulphur-depleted vapour phase. The condensed sulphur may then be recycled to the reaction zone. The sulphur-depleted vapour phase may be 10 condensed to obtain the liquid stream comprising carbon disulphide. It will be appreciated that the desired composition of the liquid stream comprising carbon disulphide will determine the condensation and/or further purification steps needed. For the conventional 15 applications of carbon disulphide, for example its use as raw material for rayon production or as solvent, a high purity of carbon disulphide is desired. If the liquid stream is used for enhanced oil recovery, i.e. for injecting it in an oil reservoir for increasing the oil 20 production from that reservoir, the liquid carbon disulphide stream may comprise substantial amounts of other components such as hydrogen sulphide and hydrocarbonaceous compounds. The liquid stream comprising carbon disulphide that 25 is formed in the process according to the invention is particularly suitable to be used in enhanced oil recovery, since the liquid stream typically comprises components other than carbon disulphide that do not need to be removed for this application. Therefore, the 30 process according to the invention preferably further comprises injecting the liquid stream comprising carbon disulphide into an oil reservoir for enhanced oil recovery. The liquid stream comprising carbon disulphide may be mixed with other liquid components or streams 35 before being injected into the oil reservoir.
WO2007/131976 PCT/EP2007/054610 -8 Typically, the liquid stream comprising carbon disulphide obtainable by the process according to the invention will also comprise hydrogen sulphide dissolved in the carbon disulphide, usually in a concentration in 5 the range of from 0.1 to 66 wt% hydrogen sulphide based on the weight of carbon disulphide. Such a liquid stream comprising carbon disulphide and hydrogen sulphide is particularly suitable for enhanced oil recovery. Therefore, the invention further provides the use of a 10 liquid stream comprising carbon disulphide and hydrogen sulphide obtainable by the process according to the invention for enhanced oil recovery. Examples In a quartz reactor tube (inner diameter 12 mm; 15 length 40 mm) an amount of powdered elemental sulphur is loaded. The reactor is brought at a pressure of 10 bar (absolute) with a flow of nitrogen and the reactor is heated to a reaction temperature above 400 oC. At the reaction temperature, the reactor tube was filled with a 20 liquid sulphur column with a height of 15 cm. A gaseous mixture comprising a hydrocarbon (methane or ethane) was supplied to the bottom of the reactor. At the top of the reactor, a gaseous effluent was withdrawn. The composition of the gaseous effluent was analysed by gas 25 chromatography. Seven different experiments were carried out. In the Table, the reaction conditions and the results are given for experiments 1 to 7.
WO 2007/131976 PCT/EP2007/054610 Q 0 U0) 0) 0 0 00 E D ID L 0 C o 0\ 0 Q (Y * ~ f U0) cl0) 04 01 41C r ) ' 04-4 N 2N N N N U) 4 00. rj 0 0r 44-) ~ O > CN 0 0 0 co c o 00 N~ CD U) 0 H P4 71~ a)1 r C;I 0 0) : x 0 U 0 1j (N C)0 C .H w0 0) 4J 0) 4H 4- -P CD 4 0~~~> r D I 1 C" H 0 H 0 0 0- ' ' Q) 'd -. C CO C)C4- 0 0 , QH 0 W a)i~ C ( i c 0 i~ m V Ln P)
Claims (10)
1. A process for the manufacture of carbon disulphide comprising supplying a feedstock comprising a hydrocarbonaceous compound to a reaction zone containing a liquid elemental sulphur phase and reacting, in the 5 liquid sulphur phase, at a temperature in the range of from 350 to 750 'C and a pressure in the range of from 3 to 200 bar (absolute) and in the absence of a catalyst, the hydrocarbonaceous compound with elemental sulphur in the absence of molecular oxygen. 10
2. A process according to claim 1, wherein the feedstock comprising the hydrocarbonaceous compound is introduced into the liquid sulphur at the lower end of the reactor.
3. A process according to claim 1 or 2, wherein the hydrocarbonaceous compound is a compound that is gaseous 15 at the reaction conditions.
4. A process according to any of claims 1 to 3, wherein the hydrocarbonaceous compound is a hydrocarbon, preferably a saturated or unsaturated aliphatic hydrocarbon, more preferably an aliphatic hydrocarbon 20 with up to 20 carbon atoms, more preferably a saturated aliphatic hydrocarbon with up to 4 carbon atoms.
5. A process according to any one of the preceding claims, wherein the temperature in the reaction zone is in the range of from 400 to 700 'C, preferably of from 25 400 to 650 oC.
6. A process according to any one of the preceding claims, wherein the pressure in the reaction zone is in the range of from 3 to 200 bar (absolute), preferably of from 5 to 100 bar (absolute), more preferably of from 5 30 to 30 bar (absolute).
7. A process according to any one of the preceding claims, further comprising withdrawing a gaseous phase WO2007/131976 PCT/EP2007/054610 - 11 comprising carbon disulphide and hydrogen sulphide from the reaction zone, condensing at least part of the gaseous phase to obtain a liquid stream comprising carbon disulphide. 5
8. A process according to claim 7, further comprising injecting the liquid stream comprising carbon disulphide into an oil reservoir for enhanced oil recovery.
9. Use of a liquid stream comprising carbon disulphide and hydrogen sulphide obtainable by a process according 10 to claim 7 for enhanced oil recovery.
10. Enhanced oil recovery process using carbon disulphide, optionally combined with hydrogen sulphide, manufactured according to the process of any of claims 1 to 7.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP06114011 | 2006-05-16 | ||
EP06114011.7 | 2006-05-16 | ||
PCT/EP2007/054610 WO2007131976A1 (en) | 2006-05-16 | 2007-05-14 | A process for the manufacture of carbon disulphide |
Publications (1)
Publication Number | Publication Date |
---|---|
AU2007251608A1 true AU2007251608A1 (en) | 2007-11-22 |
Family
ID=37067536
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
AU2007251608A Abandoned AU2007251608A1 (en) | 2006-05-16 | 2007-05-14 | A process for the manufacture of carbon disulphide |
Country Status (10)
Country | Link |
---|---|
US (1) | US20090155159A1 (en) |
EP (1) | EP2018349A1 (en) |
CN (1) | CN101443269B (en) |
AU (1) | AU2007251608A1 (en) |
BR (1) | BRPI0711058A2 (en) |
CA (1) | CA2651953A1 (en) |
EA (1) | EA014708B1 (en) |
MX (1) | MX2008014282A (en) |
NO (1) | NO20085244L (en) |
WO (1) | WO2007131976A1 (en) |
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US8459368B2 (en) | 2006-04-27 | 2013-06-11 | Shell Oil Company | Systems and methods for producing oil and/or gas |
EA014709B1 (en) | 2006-05-16 | 2011-02-28 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | A process for the manufacture of carbon disulphide |
US8136590B2 (en) | 2006-05-22 | 2012-03-20 | Shell Oil Company | Systems and methods for producing oil and/or gas |
EP2038219A1 (en) | 2006-07-07 | 2009-03-25 | Shell Internationale Research Maatschappij B.V. | Process for the manufacture of carbon disulphide and use of a liquid stream comprising carbon disulphide for enhanced oil recovery |
CN101501295B (en) | 2006-08-10 | 2013-11-20 | 国际壳牌研究有限公司 | Methods for producing oil and/or gas |
CA2676231A1 (en) | 2007-02-16 | 2008-08-21 | Shell Internationale Research Maatschappij B.V. | Systems and methods for absorbing gases into a liquid |
WO2009012374A1 (en) | 2007-07-19 | 2009-01-22 | Shell Oil Company | Methods for producing oil and/or gas |
CA2703888A1 (en) | 2007-10-31 | 2009-05-07 | Shell Internationale Research Maatschappij B.V. | Systems and methods for producing oil and/or gas |
WO2009067423A1 (en) | 2007-11-19 | 2009-05-28 | Shell Oil Company | Producing oil and/or gas with emulsion comprising miscible solvent |
US8869891B2 (en) | 2007-11-19 | 2014-10-28 | Shell Oil Company | Systems and methods for producing oil and/or gas |
RU2498055C2 (en) | 2008-02-27 | 2013-11-10 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Oil and/or gas extraction system and method |
RU2494239C2 (en) | 2008-04-16 | 2013-09-27 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Oil and/or gas extraction system and method |
EA201100957A1 (en) * | 2008-12-15 | 2011-12-30 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | METHOD FOR HANDLING HYDROCARBON RAW MATERIAL TREATMENT TO REDUCE ITS VISCOSITY |
CN108483446B (en) * | 2018-04-10 | 2021-12-10 | 上海东庚化工技术有限公司 | Method and system for separating excessive sulfur in carbon disulfide production process |
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-
2007
- 2007-05-14 AU AU2007251608A patent/AU2007251608A1/en not_active Abandoned
- 2007-05-14 MX MX2008014282A patent/MX2008014282A/en unknown
- 2007-05-14 EP EP07729062A patent/EP2018349A1/en not_active Withdrawn
- 2007-05-14 BR BRPI0711058-8A patent/BRPI0711058A2/en not_active IP Right Cessation
- 2007-05-14 WO PCT/EP2007/054610 patent/WO2007131976A1/en active Application Filing
- 2007-05-14 CN CN2007800176223A patent/CN101443269B/en not_active Expired - Fee Related
- 2007-05-14 EA EA200802327A patent/EA014708B1/en not_active IP Right Cessation
- 2007-05-14 CA CA002651953A patent/CA2651953A1/en not_active Abandoned
- 2007-05-14 US US12/300,759 patent/US20090155159A1/en not_active Abandoned
-
2008
- 2008-12-15 NO NO20085244A patent/NO20085244L/en not_active Application Discontinuation
Also Published As
Publication number | Publication date |
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CA2651953A1 (en) | 2007-11-22 |
US20090155159A1 (en) | 2009-06-18 |
NO20085244L (en) | 2008-12-15 |
EA200802327A1 (en) | 2009-04-28 |
EA014708B1 (en) | 2011-02-28 |
EP2018349A1 (en) | 2009-01-28 |
CN101443269B (en) | 2012-06-27 |
MX2008014282A (en) | 2008-11-18 |
CN101443269A (en) | 2009-05-27 |
BRPI0711058A2 (en) | 2011-08-23 |
WO2007131976A1 (en) | 2007-11-22 |
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